Material treatment systems for waste destruction, energy generation, or the production of useful chemicals

ABSTRACT

A system for treating a feedstock for the purposes of waste destruction, energy generation, or the production of useful chemicals is disclosed and includes a reactor vessel. A heating lance is configured to outflow the products of a partial oxidation reaction into a reaction chamber in the vessel. The hot reaction products heat and pyrolyze the feedstock in the chamber generating a process effluent which typically includes gases (e.g. syn-gas) and carbon solids. Glasses and metals in the feedstock accumulate in the chamber in a molten state. The molten materials store thermal energy and provide thermal stability to the treatment system. A recycle loop uses carbon solids from the process effluent as an input to the lance for reaction with an oxidant therein.

The U.S. Government has a paid-up license in this invention and theright in limited circumstances to require the patent owner to licenseothers on reasonable terms as provided for by the terms of Contract No.FA8651-04-C-0158 awarded by the United States Air Force.

FIELD OF THE INVENTION

The present invention pertains generally to systems and methods fortreating materials for the purposes of waste destruction, energygeneration, or the production of useful chemicals. More specifically,the present invention pertains to efficient systems and methods fortreating waste materials having organic constituents. The presentinvention is particularly, but not exclusively, useful as a system andmethod for pyrolyzing a feed material and using the resulting carbonsolids in a recycle loop to heat and pyrolyze incoming feed material.

BACKGROUND OF THE INVENTION

The long-term storage of waste in landfills can be problematic forseveral reasons. First, landfill space is limited. On the other hand,the production of waste materials seems to be increasing at anever-incredible pace. Moreover, conventional landfills can pose seriousenvironmental problems including the contamination of nearby groundwaterand the generation of air pollutants. Unfortunately, the treatment andrecycling of most conventional forms of waste remains a seriouschallenge. As a minimum, an effective treatment/recycling solution mustbe energy efficient and present minimal environmental risks.

In general, conventional treatment/recycling schemes have been somewhatlimited when applied to mixed wastestreams and wastestreams that includebulk solids. For example, consider a continuous feed, high pressuresystem for processing waste. The pressurized nature of these processestypically requires that bulk solids be ground to a fine particle size toallow the pumping of the particularized solids into a high pressurereactor. Both grinding and pumping can require specialty equipment. Inparticular, a different device is generally required for differentmaterials such as wood, plastic, or friable solids. Once the materialhas been ground, introduction into a pressurized reactor usuallyrequires slurrying the material at a high concentration to minimize thesize of the reactor and associated process equipment. Thus, expensive,high pressure slurry pumps for viscous streams are typically required.For other solids such as metals, glass or ceramics, suitablesize-reduction for introduction into a pressurized reactor vessel isgenerally impractical.

In addition to conventional wastestreams, a large amount of waste isgenerated each year that is hazardous and cannot be placed in aconventional landfill unless it is pre-treated. Among this hazardouswaste is a large amount of mixed waste consisting of non-hazardoussolids that are contaminated with hazardous constituents. Examples ofsuch mixed wastes include soils, inorganic adsorbents and other solidsthat are contaminated with hazardous organic materials. Another suchmixed waste consists of conventional and chemical munitions as well asmunition dunnage. Protective suits, munition bodies and equipmentcontaminated with energetics, biological or chemical warfare agents isanother mixed waste that cannot be safely placed in a conventionallandfill without pretreatment. Similarly, PCB contaminated transformers,pesticide contaminated bags and containers, medical/biohazard waste suchas contaminated needles and glass containers, and computer waste thatcan include lead and other hazardous materials are all mixed wastes thatcannot be safely placed in a conventional landfill.

Another factor that must be considered when contemplating thetreatment/recycling of materials is the generation of treatmentby-products that can present handling difficulties and in some casesinterfere with the treatment process. For example, when supercriticalwater oxidation (SCWO) type processes are used to treat wastestreams,sticky solids are often generated that can plug a reactor vessel, absentspecial precautions. In a similar manner, when low and moderatetemperatures are used as part of a treatment process, organics that arepresent in a wastestream often generate tars which are difficult tohandle and process. Similarly, partial oxidation gasification systemstypically generate dirty process effluents and can be difficult tocontrol because of variations in the heat capacity, water content, andreactivity of the wastes.

Perhaps the most important consideration when considering thetreatment/recycling of waste is the energy required to process thewaste. Depending on the process, significant amounts of energy may berequired to heat the waste, pressurize or depressurize a reactor vessel,and/or mix and transport the waste. Heretofore, processes such as plasmaarc pyrolysis and other electrically heated systems have typicallyrequired large amounts of power to heat and vaporize the waste. For thisreason, these processes typically cannot generate net power and as aconsequence have not been widely adopted.

In light of the above, it is an object of the present invention toprovide systems and methods suitable for the purposes of efficientlytreating feedstocks such as wastestreams which do not generate stickysolids or tars. It is another object of the present invention to providesystems and methods for treating feedstocks for the purpose of wastedestruction, energy generation, or the production of useful chemicals.Yet another object of the present invention is to provide systems andmethods for chemically converting feedstocks which are energy efficient,simple, and economical.

SUMMARY OF THE INVENTION

The present invention is directed to systems and methods for treating afeedstock for the purposes of waste destruction, energy generation, orthe production of useful chemicals. For the treatment system, a reactorvessel is provided that is formed with a reaction chamber. The vessel isfurther formed with one or more inlets to allow the feedstock to beintroduced into the reaction chamber. In addition to the inlet, thereactor vessel is formed with an opening to allow a heating lance tooutflow the products of an oxidation reaction into the reaction chamber.These hot reaction products outflowing from the lance are used to heatthe feedstock and pyrolyze organics in the feedstock. In quantitativeterms, the reaction chamber is generally maintained at temperaturesabove about 1100 degrees Celsius for most types of feedstocks, and istypically maintained between 1300 and 1600 degrees Celsius.

Pyrolysis of the feedstock in the reaction chamber generates a processeffluent which typically includes, but is not necessarily limited to,syn-gas and carbon solids. If present, solid glasses and metals in thefeedstock melt upon exposure to the hot reactor chamber and accumulateat the bottom of the chamber. The accumulated molten glass and metalefficiently store thermal energy and provide thermal stability to thetreatment system.

For the treatment system, a recycle loop is established to introducecarbon solids from the process effluent into the lance for oxidationtherein. In greater detail, the process effluent, which includes gasesand carbon solids, is evacuated from the reaction chamber, for example,using a blower. In one embodiment, the carbon solids are then separatedfrom the process effluent using a baghouse. From the baghouse, thecarbon solids are introduced into the heating lance for reaction with anoxidant, such as oxygen, from an oxidant source.

In a particular implementation of the treatment system, asub-stoichiometric amount of oxidant is introduced into the lance whichresults in a partial oxidation of the carbon solids therein. Moreover,the lance inputs are generally controlled such that the reaction betweenthe oxidant and carbon solids is completed in the lance and prior to theoutflow of reaction products from the lance into the reaction chamber.Thus, for this implementation, the reaction chamber can be maintained inan overall net-reducing state.

In one embodiment of the treatment system, the blower draws the processeffluent through a plasma polisher which pyrolyzes any gaseous organicmolecules that are present in the process effluent. Typically, theblower maintains the pressure inside the reactor chamber atsub-atmospheric levels. From the plasma polisher, the effluent can becooled and then sent to the baghouse for removal of the carbon solids.In addition, heat can be exchanged between the hot process effluent andthe colder feedstock that is entering the reaction chamber. In somecases, gases exiting the baghouse are treated to remove acids. Theremaining gases are then further processed. For example, hydrogen can beisolated from the remaining gases and stored for subsequent use as aproduct of the process. If desired, the syn-gas can be compressed andstored for subsequent use. In one implementation, the syn-gas can beinput into the lance to supplement the carbon solids in the partialoxidation reaction. Alternatively, or in addition thereto, the syn-gascan be used to stir the molten materials in the reaction chamber. Thisstirring can be used to increase the heat transfer to the incomingfeedstock. Also, gases from the separator can be used to drive an engineor turbine. Moreover, the waste heat from the engine/turbine can be usedto heat, and in some cases, dry the feedstock entering the reactorchamber.

BRIEF DESCRIPTION OF THE DRAWINGS

The novel features of this invention, as well as the invention itself,both as to its structure and its operation, will be best understood fromthe accompanying drawings, taken in conjunction with the accompanyingdescription, in which similar reference characters refer to similarparts, and in which:

FIG. 1 is a schematic diagram of a treatment system showing the systemcomponents and flow paths for the various system reactants and products;

FIG. 2 is a schematic diagram of another embodiment of a treatmentsystem having an apparatus for compressing and storing syn-gas and anapparatus for separating and storing hydrogen gas from the processeffluent;

FIG. 3 is a schematic diagram of yet another embodiment of a treatmentsystem having a heat exchanger for using the hot reactor effluent toheat and dry the feedstock; and

FIG. 4 is a schematic diagram of still another embodiment of a treatmentsystem having a gas cooler and heat exchanger which cooperate to heatthe feedstock in a controlled manner using heat from the hot reactoreffluent.

DESCRIPTION OF THE PREFERRED EMBODIMENTS

Referring initially to FIG. 1, a treatment system is shown and generallydesignated 10. As shown, the system 10 includes a reactor vessel 12 thatis formed with a reaction chamber 14. FIG. 1 shows the reactor vessel 12during a typical steady state operation. During this operation, it canbe seen that the chamber 14 contains a molten metal layer 16, a moltenglass layer 18 and a headspace 20 above the molten layers 16, 18. It canbe further seen from FIG. 1 that a feedstock 22 is introduced into theheadspace 20 via an inlet 24. Although one inlet 24 is shown, it is tobe appreciated that the vessel 12 can be formed with two or morefeedstock inlets 24 to allow for improved mixing, improved feed rate orimproved heat transfer between the molten layers 16, 18 and thefeedstock 22. FIG. 1 also shows that the system 10 includes a heatinglance 26 having an outflow end 28 that is positioned in the headspace 20of the reaction chamber 14.

For the system 10, the feedstock 22 typically contains an organic (i.e.carbon based) material and can include one or more waste materials, oneor more raw materials, or combinations thereof. Waste materials caninclude, but are not limited to, municipal solid waste including wastespecific streams (e.g. computer waste, battery waste, medical waste,etc.), sewage, biologically digested sewage, biological sludge andregulated hazardous wastes. Alternately, or in addition to wastematerials, the feedstock 22 can include one or more raw materials suchas an oil-based hydrocarbon. It is to be appreciated that the feedstock22 can be processed for one or more purposes to include treating and/orrecycling of waste materials, the production of energy (e.g. net power)and the generation of usable chemicals (e.g. hydrogen, syn-gas, glass,metal, etc.).

Continuing with FIG. 1, the feedstock 22 is introduced into the chamber14 where it is rapidly heated by the hot reaction products generated bythe lance 26 and the heat contained in the molten layers 16, 18. For thesystem 10, the reaction chamber 14 is generally maintained at atemperature above about 1100 degrees Celsius for most types offeedstocks 22 and is typically maintained between about 1300 and 1600degrees Celsius. Introduction of the feedstock 22 into the hot reactionchamber 14 can result in one or more reactions to include pyrolysis,gasification and vitrification reactions. In general, the rapid heatingof the feedstock 22 avoids the formation of tars (i.e. complex organiccompounds and hydrocarbons) and ensures the complete destruction ofwastes. These reactions generate a process effluent 30 which is thenevacuated from the headspace 20 by a blower 32. In most cases, theblower 32 is configured to maintain the pressure inside the reactorchamber 14 at slightly sub-atmospheric levels. Typically, the processeffluent 30 includes, but is not necessarily limited to, syn-gas andfine, divided carbon solids. When glasses and/or metals are present inthe feedstock 22, these materials typically melt upon exposure to theheat in the reactor chamber 14 and accumulate at the bottom of thechamber 14 as layers 16, 18. The accumulated molten glass and metalfunctions to trap inorganic materials in the melt, efficiently storethermal energy and provide thermal stability to the treatment system 10.The molten glass and metal can be periodically removed from the vessel12. For example, the vessel 12 can be formed with one or more holes (notshown) that accommodate removable plugs (e.g. clay plugs). In addition,the vessel 12 can include a heater, such as an induction heater (notshown), to maintain the molten layers 16, 18 at a preselectedtemperature.

As further shown in FIG. 1, the process effluent 30 exiting the chamber14 is first drawn into a gas cooler 34 which reduces the temperature ofthe process effluent 30. From the gas cooler 34, the cooled processeffluent 36 is directed into a baghouse 38 where the finely dividedcarbon solids 40 are separated from the remaining gases 42. From thebaghouse 38, the filtered gases 42 pass through the blower 32 and aredirected toward a treatment unit 44 where the gases 42 are conditionedby wet or dry removal of acid gases. The conditioned gas 46 exiting theunit 44 is then used (e.g. burned) to produce mechanical energy in anenergy conversion device 48, which is typically an engine or turbine.

With continued reference to FIG. 1, it can be seen that the carbonsolids 40 from the baghouse 38 are held in a hopper (not shown) andthereafter fed in a controlled fashion into the heating lance 26.Transport to the lance 26 from the hopper can be accomplished, forexample, using a fluidizing carrier. In one implementation, syn-gas fromthe reactor effluent 30 can be used to fluidize and transport the carbonsolids 40 to the lance 26. In the lance 26, the finely divided carbonsolids 40 are reacted with an oxidant 50 from an oxidant source 52.Suitable carbon lances for use in the system 10 can be obtained fromProcess Technology Intl., headquartered in Tucker, Ga.

Typically, for the system 10, a sub-stoichiometric amount of oxidant 50is introduced into the lance 26 which results in a partial oxidation ofthe carbon solids 40 therein. Also, the lance 26 inputs are generallycontrolled such that the reaction between the oxidant 50 and carbonsolids 40 is completed in the lance 26 and prior to outflow of thepartial oxidation products into the reactor chamber 14. Because theoxidation reactions come to completion in the lance 26, the variabilityof the feedstock 22 does not significantly affect the thermalperformance of the lance 26. The outflow stream from the lance 26typically consists of jet of carbon monoxide and carbon dioxide withlittle or no free oxidizers entering the chamber 14. With this control,the lance 26 provides a stable, adjustable heat source while allowingthe reactor chamber 14 to be maintained in an overall net-reducingstate. Although only one lance 26 is shown, it is to be appreciated thattwo or more lances 26 can be used in the system 10 and that the jet(s)from the lance(s) 26 can be directed into the molten layers 16, 18 tostir the melt and increase heat transfer from the melt to the incomingfeedstock 22.

FIG. 2 shows another embodiment of a treatment system (generallydesignated system 110). For this embodiment, the system 110 includes areactor vessel 112 that is formed with a reaction chamber 114 which, inoperation, typically contains a molten metal layer 116, a molten glasslayer 118 and establishes a headspace 120 above the molten layers 116,118. The feedstock 122 is introduced into the chamber 114 where it israpidly heated by the heat generated by the lance 126 and the heatcontained in the molten layers 116, 118. A process effluent 130, whichtypically includes syn-gas and fine, divided carbon solids, is generatedand is evacuated from the headspace 120 by a blower 132.

As further shown in FIG. 2, the process effluent 130 exiting the chamber114 is first drawn into a plasma polisher 154 by the blower 132. At theplasma polisher 154, gaseous organic molecules in the process effluent130 are reduced and pyrolyzed by a plasma arc. Because the processeffluent 130 is relatively hot entering the plasma polisher 154, plasmaenergy input requirements to heat the effluent 130, vaporize volatilesand melt solids are typically greatly reduced. FIG. 2 further shows thatthe polished effluent 156 exiting the plasma polisher 154 is drawn intoa gas cooler 134 which reduces the temperature of the process effluent130. From the gas cooler 134, the cooled process effluent 136 isdirected into a baghouse 138 where finely divided carbon solids 140 areseparated from the remaining gases 142 and directed to the heating lance126. It is to be appreciated that recycled carbon 140 can besupplemented by adding additional carbon feed material, such as coke.From the baghouse 138, the filtered gases 142 pass through the blower132 and are directed toward a treatment unit 144 wherein the gases 142are conditioned by wet or dry removal of acid gases. The conditioned gas146 exiting the unit 144 is then directed to a tee 158.

Continuing with FIG. 2, the tee 158 allows a portion or all of theconditioned gas 146 to be directed to a syn-gas compressor 160 whichcompresses the syn-gas for subsequent storage and use. Two such uses ofthe syn-gas are shown in FIG. 2. In particular, syn-gas 162 can beintroduced, alone or with fuel gas, into the lance 126 for reaction withthe oxidant 152, as shown. The fuel gas is typically used to stabilizethe reaction in the heating lance 126 and for system start-up. Inaddition, the syn-gas can be used to purge ports such as the inlet tothe reactor chamber 114 and can be introduced into the reaction chamber114 to stir the molten layers 116, 118, for example, using a wand 164.In one implementation, a portion of the effluent gas 130 is bubbledthrough the melt to mix the molten materials therein. Also, a smallamount of air or oxygen can be injected below the melt surface to mixthe melt and to oxidize carbon in the melt either directly orindirectly. An example of indirect oxidation can include the directoxidization of iron followed by the oxidation of carbon in a reductionreaction with the iron oxides. In addition, the syn-gas from the processcan be used to produce other useful compounds via thermal integrationwith basic process.

FIG. 2 also shows that the tee 158 allows a portion or all of theconditioned gas 146 to be directed to a hydrogen separation unit 166which separates hydrogen 168 from the remaining gases 170 for subsequentstorage and use. As shown, the gases 170 can be used to producemechanical energy in an energy conversion device 148, which is typicallyan engine or turbine. The engine, in turn, can be used to power thehydrogen separation unit 166. FIG. 2 also shows that the waste heat 172produced by the energy conversion device 148 can be used to dry andpreheat the feedstock 122 in a preheat exchanger 174. Typically, thepreheat exchanger 174 is controlled to heat the feedstock 122 attemperatures less than about 250 degrees Celsius to avoid gasificationand the formation of tars (which can occur during slow heating at highertemperatures). In one implementation, the waste heat 172 is used toproduce steam as a heat transfer medium to ensure that the flow of heatto the feedstock 122 is at an appropriate temperature.

FIG. 3 shows a third embodiment of a treatment system (generallydesignated system 210). As shown, the system 210 includes a reactorvessel 212 that is formed with a reaction chamber 214 which in a typicaloperation contains a molten metal layer 216, a molten glass layer 218and establishes a headspace 220 above the molten layers 216, 218. Afeedstock 222 is introduced into the chamber 214 where it is rapidlyheated by the lance 226 and the heat contained in the molten layers 216,218. A process effluent 230, which typically includes syn-gas and fine,divided carbon solids, is generated and is evacuated from the headspace220 by a blower 232.

As further shown in FIG. 3, the relatively hot process effluent 230exiting the chamber 214 is drawn through a heat exchanger 274 whichtransfers heat to an exchange fluid 276. The exchange fluid 276, inturn, passes through a second heat exchanger 278 and transfers heat tothe feedstock 222. This heat exchange can be used to dry and preheat thefeedstock 222. In particular, the heat exchanger 278 is controlled toheat and dry the feedstock 222 at temperatures less than about 250degrees Celsius to avoid gasification and the formation of tars (whichcan occur during slow heating at higher temperatures).

Continuing with FIG. 3, it can be seen that from the heat exchanger 274,the process effluent 230 is drawn through a gas cooler 234 which reducesthe temperature of the process effluent 230. From the gas cooler 234,the cooled process effluent 236 is directed into a baghouse 238 wherefinely divided carbon solids 240 are separated from the remaining gases242. The carbon solids 240 are directed to the heating lance 226 forreaction with oxidant 250 from oxidant source 252. From the baghouse238, the filtered gases 242 pass through the blower 232 and are directedtoward a treatment unit 244 where the gases 242 are conditioned by wetor dry removal of acid gases. The conditioned gas 246 exiting the unit244 is then directed to an energy conversion device 248 (e.g. an engineor turbine) for use in producing mechanical energy. As FIG. 3 shows, anauxiliary fuel 280 can be supplied to the energy conversion device 248to accommodate variations in the quality of the conditioned gas 246.

FIG. 4 shows a fourth embodiment of a treatment system (generallydesignated system 310). As shown, the system 310 includes a reactorvessel 312 that is formed with a reaction chamber 314 which contains amolten metal layer 316, a molten glass layer 318 and establishes aheadspace 320 above the molten layers 316, 318. A feedstock 322 isintroduced into the chamber 314 where it is rapidly heated by the lance326 and the heat contained in the molten layers 316, 318. A processeffluent 330, which typically includes syn-gas and fine, divided carbonsolids, is generated and is evacuated from the headspace 320 by a blower332.

As further shown in FIG. 4, the relatively hot process effluent 330exiting the chamber 314 is first drawn through a gas cooler 334 and thenthrough a heat exchanger 382 which transfers heat from the effluent 330to the feedstock 322. This heat exchange can be used to dry and preheatthe feedstock 322. In particular, gas cooler 334 and heat exchanger 382are controlled to heat and dry the feedstock 322 at temperatures lessthan about 250 degrees Celsius to avoid gasification and the formationof tars (which can occur during slow heating at higher temperatures).

Continuing with FIG. 4, it can be seen that from the heat exchanger 382,the process effluent 330 is directed into a baghouse 338 where finelydivided carbon solids 340 are separated from the remaining gases 342.The carbon solids 340 are directed to the heating lance 326 for reactionwith oxidant 350 from oxidant source 352. From the baghouse 338, thefiltered gases 342 pass through the blower 332 and are directed toward atreatment unit 344 where the gases 342 are conditioned by wet or dryremoval of acid gases. The conditioned syn-gas 384 is then stored forsubsequent use.

While the particular Material Treatment Systems For Waste Destruction,Energy Generation, or the Production of Useful Chemicals andcorresponding methods of use as herein shown and disclosed in detail arefully capable of obtaining the objects and providing the advantagesherein before stated, it is to be understood that they are merelyillustrative of the presently preferred embodiments of the invention andthat no limitations are intended to the details of construction ordesign herein shown other than as described in the appended claims.

1. A method for treating a feedstock, the method comprising the stepsof: providing a reactor vessel having a reaction chamber; inputting thefeedstock into the reaction chamber; connecting an oxidant source to aheating lance having an outflow end; introducing carbon solids and asub-stoichiometric amount of oxidant into the lance; positioning theoutflow end of the heating lance in the reaction chamber for outflow ofpartial oxidation products including carbon monoxide and carbon dioxideinto the reaction chamber; operating the heating lance to pyrolyze atleast a portion of the feedstock and produce a process effluent forevacuation from the reaction chamber, wherein the process effluentincludes gas and carbon solids; and introducing at least a portion ofthe carbon solids generated in the operating step into the lance forpartial oxidation therein, wherein oxidation reactions come tocompletion within the lance to maintain an overall net-reducing state inthe reaction chamber.
 2. A method as recited in claim 1 furthercomprising the steps of: accumulating molten glass treatment products inthe reaction chamber; and selectively removing the products from thereaction chamber.
 3. A method as recited in claim 1 further comprisingthe steps of: accumulating molten metal treatment products in thereaction chamber; and selectively removing the products from thereaction chamber.
 4. A method as recited in claim 1 wherein thefeedstock comprises computer waste.
 5. A method as recited in claim 1wherein the feedstock comprises a raw material.
 6. A method for treatinga feedstock, the method comprising the steps of: providing a reactorvessel having a reaction chamber; disposing at least a portion of thefeedstock in the reaction chamber; connecting an oxidant source to aheating lance having an outflow end; introducing carbon solids and asub-stoichiometric amount of oxidant into the lance; positioning theoutflow end of the heating lance in the reaction chamber for outflow ofpartial oxidation products consisting of carbon monoxide and carbondioxide into the reaction chamber; operating the heating lance topyrolyze at least a portion of the feedstock and produce a processeffluent for evacuation from the reaction chamber, wherein the processeffluent includes syn-gas and carbon solids; separating the processeffluent to produce a feedstream having carbon solids; and introducingthe feedstream into the lance for partial oxidation of the carbon solidstherein, wherein oxidation reactions come to completion within the lanceto maintain an overall net-reducing state in the reaction chamber.
 7. Amethod as recited in claim 6 further comprising the step of removingacids from the process effluent.
 8. A method as recited in claim 6further comprising the step of separating hydrogen from the processeffluent.
 9. A method as recited in claim 6 further comprising the stepof compressing the effluent syn-gas.
 10. A method as recited in claim 6further comprising the step of introducing effluent syn-gas into thelance for reaction therein.
 11. A method as recited in claim 6 furthercomprising the steps of: accumulating molten material in the reactionchamber; and using effluent syn-gas to mix the molten material in thereaction chamber.
 12. A method as recited in claim 6 further comprisingthe step of using a portion of the process effluent in an engine.
 13. Amethod as recited in claim 6 further comprising the step of using aportion of the process effluent in a turbine.
 14. A method as recited inclaim 13 wherein the turbine generates waste heat and the method furthercomprises the step of using the waste heat to pre-heat a portion of thefeedstock prior to disposing the feedstock portion into the reactionchamber.
 15. A method as recited in claim 6 further comprising the stepof transferring heat from the process effluent to a portion of thefeedstock prior to disposing the feedstock portion into the reactionchamber.